Process for obtaining distilled products from petroleum and other oils.



. Au A. SMP?. PHESS- FOR OBTAINING MSYILLED PWUDUCTS Fi E @MEMS MJD@HIER GHS.

APPLICATIDN FILED DEC. 4. 19H'- 2 SHEETS-SHEET i.

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Al A. STAPP. PROCESS FOR OBTAINING DIS TILLED PRODUCTS FROM PETROLEUMAND OTHER OILS. APPucATloN FILED No.4. 1917. k Lggmg., Patented Dec.9,1919.

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ARTIE A. STAPP, OF DENVER, COLORADO. i

PROCESS FOR OBTAINING DISTILLED PRODUCTS FROM PETROLEUM AND OTHER OILS.

To all/@hom may concern Be 1t known that I, ARTIE A. STAP?, a

' citizen of the United States of America, re-

siding at the city and county of Denver' and State of Colorado, haveinvented a new and useful Process for Obtaining Distilled l Productsfrom Petroleum and other Oils, of which the following is aspecification.

My invention relates to a new process for obtaining distilled productsfrom petroleum and other oils.

The objects of my process are:``

First: To provide a continuously oil feeding process for obtainingdistilled products, particularly gasolene, from petroleum and other oilsby first subjecting such oils to a pre-heat suflicient to remove thelow-boiling hydrocarbons, particularly the gasolene-fraction, andcondensing it and conveying it to t a gasolene container.

Second: To provide a continuously oil feeding process that first removesthe gasolene lfraction by a low heat, and then subjects the oils tofheat of sufficient temperature to vaporize the oils, then subjects thevapors to a temperature suiicient to crack the vapor, then condensingthe cracked product and separating conveyingthe gasolene fraction t'o acontainer.

Third :v To provide a continuous oil feed process that first removes thegasolene fraction by a low heat and then subjects the oils to highertemperature suiiicient to vaporize the oils, then subjects the vapors toa temperature suiiicient to crack them, then condenses and separates thecracked product and conveys the'gasolene fraction to' a con-4 tainer,and that passes the gas through va superheaterto a vappri'zer and thenceto a cracking chamber to increase the percentage of saturatedhydrocarbons, and thus reduces the loss by gas' formation. Also, toprovide Specification of Letters Patent.

Patented Dec. 9, i919.

Application filed December 4, 1917. Serial No.4 205,419.

Fig 2 is a vertical, longitudinal, sectional view of one of thegasolene. containers.

Fig. 3 is a vertical, longitudinal, sectional view of the vaporizer,showing a reciprocating carbon scraper therein.

Fig. 4 is a vertical, transverse, sectional View of the vaporizer,showing an end view of the scraper.

Fig. 5 is a horizontal, sectional view on the line 5-5 of Fig. 4.

Fig. 6 is a longitudinal, sectional view, showing a lcylinder andhydraulically, operated piston therein, to which the 'carbon scraper rodis secured; and

Fig. 7 is a side view embodying a slight modication in connection withthe gas superheater. Q

Similar letters of reference refer to similar parts throughout theseveral views.

M process has for its essential object'the obtaining of low boilinghydrocarbons from petroleums and heavy oils in a continuous oil feedapparatus that is arranged to remove the gasolene fraction as well as toextract benzene and other valuable products from oils, and at the sametime mechanically eliminate the deleterious carbon and other residueproducts during the operation of the process, thus enabling me toproduce gasolene and other products economically and on a large scale.Inasmuch as the apparatus herein illustrated has been especiallydesigned to effect this process,l a detailed description of the same isgiven, as follows:

The numeral 1 indicates a petroleum or other oil supply tank, which isconnected by a pipe 2, with a suitable pump 3, which is also connectedby a pipe 4, with a preheater, which constitutes the first unit Aof theimproved apparatus.

This pre-heater consists of a pipe or tube 5, of suitable dimensions, aportion of which is housed within a heater 6, in the form preferably ofa brick or other heat resisting chamber, the portion of "the tube 5,outside of the. heating chamber being provided with an asbestoswrapping, this arrangementfefL fecting a gradual heating of the oilafter entering the said pre-heater.

I may employ either oil or gas as a heating medium throughout theapparatus, and to this end a fuel pipe 8, projects into the heaterbeneath the tube 5, the pipe being arranged with suitable burners andbeing connected with a fuel supply.V The pipe 8, is provided with avalve 9, for regulating cof,

thc fuel supply. The end portion of the pipe 5, within the. heater` hasconnected therewith a vertical tube or pipe 10, which constitutes afiltering column, and the heater is constructed to inclose this columnalso. A pipe 11, extends from the column 10, and connects with acondenser coil 12, which is connected by a pipe 13, with a gasolenecontainer 14.

The filtering column is filled with any suitable material such as ironballs or broken clay, which form a condensing medium for the vapors,whereby a closer separation of the vapors at a given temperature iseffected.

A pipe 15, connects the inner end of the tube 5. with a cylindricalvaporizer 16, which is inclosed in a suitable heating chamber 17. andbeneath the vaporizer is a fuel pipe 18, having suitable burners, thepipe being connected with a fuel supply. The vaporizer has a verticaldepending outlet pipe 19, at each end and these pipes connect with aconveyer tube 20, in which is mounted a spiral conveyer 21. The carbonwhich adheres to the wall and ends of the vaporizer is removed in amanner to be here` inafter described, and passes down through the pipes19, to the tube 20, whence it is carried forward by the spiral conveyerand deposited in a container 22, which is connected to the tube 20, by avalved pipe 23. The container has a draw-off valve 24, for removing thecarbon, during which operation the valve in the pipe 23, is closed.

The heater 17, has a floor 25, beneath which the conveyer tube runs, andinner end walls 2,6, which are spaced from the main or outer..;en-dwalls. In the space between these walls arelocated the pipes 19, whichare thus shielded from the heat generated in the heating chamber. Theheaters (i and 17 are provided with outlet pipes or chimneys 27. 1

From one end of the vaporizer extends a vertical pipe 28, whichconstitutes a cracking chamber' and this pipe is preferably tapered fromits lower or inlet end to its upper or outlet end. The cracking tube 28,is surrounded throughout its length by a stack 29, having an outlet pipeor chimney at its upper end, and which is spaced all around from thecracking tube. The stack is formed at regular intervals with suitablyarranged openings 30, in which arey introduced burners 31, which areconnected to fuel pipes 32 leading to the fuel supply.

The burners 31', are adapted to raise the temperature in the crackingtube to 450 degrees C. or above, in order to break up the heavierhydrocarbons in hydrocarbons of lighter gravity. A pipe 34, extends fromthe upper end of the cracking tube and forms an outlet for the vapors insaid tube. This tube connects with a `condenser 35,

which in turn is connected by a pipe 3G, with a separator 37, which ispreferably cylindrical in form and is housed within a heater 38. Theseparator has a filtering column 39,

at one end, similar to the filtering column 10, of the pre-heater andsupplied with the same character of condensing or separating material asthe column 10, and a pipe 4() extends from the column 39 to a condenser41, which in turn connects with a gasolene container 42. A fuel burner37A, extends beneath the separator and connects with the main fuelsupply pipe.

The condensers 12 and 41 are connected by a gas conveying pipe 43, whichis connected by a pipe 44 with a pipe 45, which connects with the upperends of the containers 14 and 42. rllhe pipe 45, extends from thecontainers 14 and 42 to a suitable gas pump 46, to which is alsoconnected one end of a pipe 47, which connects at its other end with apipe 48, that forms a connection between the conveyer tube 20 and aresidue container 49.

The end of the separator 37, opposite that which receivesthe pipe 3G, isprovided with a pipe 50, which connects with the pipe 15 leading fromthe pre-heater. The pipes 15 and 50 are formed with traps 51 and 52,respectively, which collect any carbon passing from the pre-heater andseparator respectively. The pipes 15 and 50 are also connected by a gasconveying pipe 53, which in turn is connected by a branch pipe 54, withthe gas pipe 47, and the pipe 47 has a branch 100 pipe 55, which leadsto one end of a superheater 56, the other end of which is connected by apipe 57, with the vaporizer 1G.

A fuel burner 58, extends beneath the superheater 56, and is connectedwith the fuel supply. rlhe gases passino through the pipe 47 enter' thesuperheater through the branch pipe 55, and are there subjected to ahigh temperature by contact with incandescent carbon in the said heaterafter which they pass through the pipe 57 into the vaporizer, when theymix with the vapors therein and pass into the cracking tube, where thepresence of such gas revents the formation of gas of the sameclihracter, thus maintaining a state of equilibrium in the action of thecracking tube, the reaction tending toward the formation of low boilinghydrocarbons instead of gas.

The gas which is released in the separator passes through pipes 40, 43and 44, to the upper ends of both gasolene containers, whence it isdrawn away by the pump 46, and forced through the superheater 56 to thevaporizer, where it mixes with the vapors therein, which then ascends inthe cracking tube, increasing the percentage of saturated hydrocarbonsas above stated. The vapors and gas pass up through the cracking tubeand thence through the condenser 35 to the 130 separator, the pipes 53and 54 acting to 'equalize the pressure on the opposite sides of thetraps 15 and 52. Thus a continuous circulation of the gas through theapparatus is effected by the pump 46, and a constant pressure of aboveone atmosphere is maintained by a pressure release valve 59, whichpermits escape of the gas under excessive pressure.

The oil pipe 4, leading from the oil pump 3, to the pre-heater is alsoprovided with a pressure release valve 60, which is connected by a pipe61, with the pipe 2, leading to the o1l supply tank, or if desired, thepipe 61, may connect directly with the supply tank.

The gasolene containers 14 and 42 are each constructed as shown in Fig.2, and are provided at their lower ends with draw-oft` valves-62, bywhich the carbon which settles to the rbottoms of the containers can bewithdrawn. These containers are also provided with spigots 63, which areconnected to the outer ends of threaded nipples 64, on the inner ends ofwhich are screwed elbows 65, each of which is provided with a diaphragmhaving a conical aperture 66, which is adapted to be opened. or closedby a needle valve 67, which extends slidably through` an axial hole-in acap 68, which is screwed upon the upper end of the elbow. The upper endof the valve is pivotally connected to the lower end of a link 69, theupper end of which is pivotally connected to a lug on the bottom of afloat 70, which is upheld by the body of gasolene in the container. Thevalve 67 has secured thereon a stop collar 71, which yengages the cap 68and thus limits the upward movement of the valve. The vertical portionof the elbow above the diaphragm, is provided with apertures 72, throughwhich the oil flows to the'conical aperture in the diaphragm, and thenceout through the spigot. When the flow of oil into the container iscontinuous, the float is elevated and the needle valve is raised andpermits: the oil to run out through the spigot, but when th. oil in thetank drops below a certain level, the oat descends and the needle valvecloses the outlet, and prevents dripping at the spigot.

In all apparatus'for the treatment of petroleum to produce low boilinghydrocarbons, the problem of the removal of carbon, wherever it settlesand adheres, must be met, in order to insure efciency, and in thepresent apparatus I have devised the following mechanism for removingcarbon from the vaporizer, and also from the vapor pipe 34, leadingfromA the cracking tube, the mechanisms beingthe same in both places.

In Fig. 3 is illustrated an enlarged view, in section` of the vaporizer,showing the reciprocating Scrapers, and in Fig. 6 is illustratedmechanism ,for reciprocating the Scrapers. The scraping devices aremounted on a rod 73, which passes through a packing box 74, on one endof the vaporizer. Upon the end of the rod which extends into thevaporizer is secured a hub 75, having oppositely extended wing portions76, Which are provided with dove-tailed recesses, and in each of theserecesses is slid the shank portion of a scraper 77the edges of the shankbeing beveled lto fit the recess, as clearly shown in Fig. 5.

, The shanks of the Scrapers are slotted as shown in Fig. 4, and bolts78 are passed through the said slots, and through holes in the wings,and receive clamping nuts 79.

tial rotation bein'g suflicient to, rotate the scra'pers 77, a distanceequal to the length of their cutting edges, and an angle plate form ofscraper 81 is secured to the face of the i blade 80, as shown in Fig. 4,which is adapted to contact with the end plate or head of the vaporizer,and scrape a Vportion oi' the carbon therefrom on each alternate strokeof the rod.

, A hub 82 similarto the hub 75 but facing in the opposite direction, issecured upon the rod 73, at a distance fromV the first hub, slightlyless than halt1 the length of the vaporizer, and this hub is providedwith. Scrapers similar to those carried by the hub 75, with theexception that the blade corresponding to the blade is apertured toreceive the rod `73, while the end scraper corresponding to the scraper81 is formed in two parts which lie on opposite sides of the rod 73, asshown.

The rod 73 is adapted to have a stroke slightly greaterthan the distancebetween the two scraping devices, in order that each scraping device mayoverlap the path of the other at the center portion of the ,vaporizer,and thus keep the entire surface of the same free from carbon.

The outer extension of the rod 73, passes through a cylinder 83, whichis provided with a packing box at each end, and upon that portion of therod within the cylinder is rigidly mounted a piston 84 having projectinghubs on each side of the same, which engagethe heads of the cylinder, todefine a space between each cylinder head,'and the adjacent face of thepiston. Pipes 85 are screwed into threaded apertures inthe cyll Theslots permit'adjustment of the Scrapers inder adjoining their ends, andthe inner ends of these pipes are screwed into a circular valve casing86, at diametrically opposite points. This casing is also provided withan inlet pipe 87, and an outlet pipe 88, at diametrically oppositepoints, and a valve 89 is pivotally'mounted in the casing. This valve isa four-Way valve, and permits the entrance of water into one end of thecylinder back of the piston, and the exit of water from the other end ofthe cylinde-r simultaneously. A rock arm 90 is secured to the stem ofthe valve, and a rod 91 is connected to the rock arm, and any suitablemechanism for operating the rod to oscillate the valve may be employed.Any suitable means may also be employed to partially rotate the rod 73,at the limit of each stroke, andas one Way of accomplishing this, 1 mayform the rod 73 square, for a portion of its length, and have thesquared portion slide through an intermittently operated ratchet wheel92 as shown, this feature forming no part of the present invention. Bygiving to the scrapers a continuous `reciprocating movement, togetherwith a partial rotation at the end of each stroke, the Whole interiorsurface of the vaporzer is kept free from carbon deposit, and the carbonthus removed passes down through the pipes 19, and into the conveyerpipe 20, where it is carried by the conveyor 21 to the container 22. Theresidue, which is a tarry substance, passes from the conveyor pipe upthrough the pipe 48, and into a container, whence it may be drawn oii'from time to time. n

In Fig. 7, the superheater and vaporizer are shown connected by a pipe57A, a part of which is in the form of a condenser' 57B, for thecondensation of any liquids formed in the superheater.

The first operative step of my process consists of automatically feedingpetroleum oils to a heater which I term a pre-heater, Where thetemperature is only sufficient to release from the oil the low boilinghydrocarbons, particularly the gasolene fraction.

The second step comprises means herein described for passing theliberated gasolene product to a condenser 12, and then to a gasolenecontainer 14.

The third step consists of means including a pump for drawing the gasfrom the con denser and gasolene container and forcing the same into andthrough a gas superheater to a vaporizer, or from the superheaterthrough a condenser and thence to the vaporizer, depending upon liquidformation in the superheater.

This gas superheater and the pump and piping form a coperating part of asecond condenser 41 and gasolene container 42, which Will beparticularly referred to hereinafter.

The fourth step of my process is to then convey the oil from apre-heater, horizontally arranged, to a vaporizer 16, that is providedwith a cracking chamber 28.

The vaporizer is surrounded by a heater 17 and the cracking chamber issurrounded by a stack 29, and both the stack and the heater are providedwith gas heating apparatus for securing and maintaining the requiredtemperature.

The vapors arising in the cracking tube are converted by the crackingprocess into a mixture of gases and low and high boiling hydrocarbons,which pass from the cracking tube, through the condenser 35, and intothe separator 37, Where the temperature is such that a separation of thehydrocarbons takes place, the low boiling product passing through thefiltering column 39, pipe 40, and condenser 41, to the container 42,While the high boiling product is returned to a vaporizer for furthertreatment, the uncondensed gases being conveyed to the superheater, andthence to the vaporizer.

The next step is then to convey the oil products from the separator tothe vaporizer 1G or to one heated to a diiierent temperature, which isdone through a pipe 50, which connects 'with the pipe 15 that leads fromthe pre-heater. The gas in the containers 14 and 42, is thus drawnthrough the pipe 45 by the pump 4G, and is forced through the pipes 47and 55 to the superheater 56.

The vaporizer 16, as Well as the pipe leading from the cracking chamberto the condenser 35, is provided with suitable carbon loosening andejecting apparatus.

The next step is then to superheat the gas in the superheater 56, Whichis done by a suitable gas burner 58, and to then convey this superheatedgas directly into the vaporizer 16, or rst pass it through a condenseras before mentioned, and then to the vaporizer. The superheater is alsoconnected to the residue receptacle 49, and with the conveyertube 20,through the pipe 48.

The superheated gas from the pre-heater and the separator is forced bythe pump 46, into the vaporizer, Where it miXesWith the vapors therein,thereby subsequently increasing the percentage of saturatedhydrocarbons, and these mixed gases and vapors pass up through thecracking tube under a continuously increasing temperature, andv thencethrough the condenser 35 to the separator, and from it to the condenser41, and to the gesolene container 42.

A pressure release valve 59 is placed in the gas circulating system,that permits the pump to maintain a constant pressure of about one ormore atmospheres.

My process provides a simple, easily and economically operated processfor the treatment of petroleum oils to produce loW boiling hydrocarbonssuch as gasolene and other products therefrom, as set forth in thetreatment embodying theessential steps of my process.

I do not, however, wish to be limited in them or to the exact operationof them as described, as changes might be made without departing from myinvention.

Having described my process, what I claim as new and desire to secure.by Letters Patent, is z' The herein described process of continuouslyproducing low boiling hydrocarbons, as kerosene, benzin and gasolenefrom petroleum oils, which consists of first treating the oil to atemperature suiiicient only to release the gasolene fraction, thencondensing the gasolene in said fraction and separating the same fromthe uncondensed gas which is subjected to further treatment as set forthbelow, then vaporizing the heavy oil, and cracking and condensing andsepa rating the low and high boiling hydrocarbons, condensing thegasolene fraction, then superheating the separated gas together withthat previously mentioned, and mixing the same with the vaporsundergoing the cracking treatment.

In testimony whereof I atlix my signature in presence of two witnesses.

ARTIE A. STAPP.

Witnesses:

G. SARGENT ELLIOTT, ELIZABETH SMITH.

